Schematic representation of batch

Fig. 3 Schematic representation of batch-wise passive membrane dialysis (A) and continuous membrane filtration dead-end-filtration (B) and loop reactor (C)...

FIGURE12.4 Schematic representation of batch preparation of functionalized thermally sensitive poly(NIPAM) microgel particles. NIPAM(lg)/MBA(<10% w/w)A 50(0.1 w/w%). The preparation of such poly(alkylacrylamide) particles can only be performed for low solid content, generally less than 5% w/v. V50 2-2 azo-bis amidinopropane dihydrochloride, MBA methylene bis acrylamide, AEMH amino-ethyl methacrylate hydrochloride. 

FIGURE 4.1. Schematic representation of batch reactors, (a) Without recirculation (PV= working electrode, C = counter electrode, S = separator) (b) with recirculation. (Vg = reactor volume, V, = reservoir volume). 

FIGURE 9.5 Schematic representation of batch preparation of functionalized thermally sensitive poly(NIPAM) microgel particles. Basically, to perform such polymerization by a non-polymer chemistry scientist, this recipe based on 1 g of NIPAM, 0.12 g of MBA, 0.012 g of KPS, and 50 mL water in closed battle and placed at 70°C leads to monodisperse microgel particles. 

Figure 4.1 Schematic representation of batch (a) and semi-batch operation (b).

Schematic representation of concentration in solution, C, as a function of distance from the surface of the dissolving mineral. In the lower part of the figure, the change in concentration (e.g., in a batch dissolution experiment) is given as a function of time.

Fig. 10. Schematic representation of optical/MAS NMR probe for photocatalytic investigations under batch reaction conditions. Reproduced with permission from (52). Copyright 1998 American Chemical Society.

Figure 13.1 Schematic representation of a fully instrumented bioreactor system for an industrial-scale fed-batch culture (solid line - fluid flow and air flow dotted line - ana-log/digital signals).

Fig. 10.5 Photograph and cross-sectional schematic representation of a Banbury high-intensity internal batch mixer. The photograph shows the two elements of the drive the electrical motor and the gear reducer. Their large size is due to the very large power requirements of the mixer. [Photograph courtesy of the Farrel Company, Ansonia, CT.]...

Fig. 8.7 Schematic representation of the contact-free batch reactor (CFBR). L MP Hg lamp =...

Figures 22a, b provides a schematic representation of the pilot scale reactor. Essentially it is a rectangular parallelepiped limited by two parallel windows made of borosilicate glass and operated as a slurry reactor inside the loop of a batch recycling system. Irradiation of one of the reactor faces is obtained using two tubular lamps that were placed along the focal axis of two parabolic reflectors made of specularly finished aluminum (Brandi et al., 1996, 1999, 2002). The specific information concerning the experimental device is presented in Table 9, and more details can be found in Satuf et al. (2007b).

FIGURE 6.20 Schematic representation of a batch filtration system. 

Figure 13.5. Transport vs surface controlled dissolution. Schematic representation of concentration in solution, C, as a function of distance from the surface of the dissolving mineral. In the lower part of the figure, the change in concentration (e.g., in a batch dissolution experiment) is given as a function of time, (a) Transport controlled dissolution. The concentration immediately adjacent to the mineral reflects the solubility equilibrium. Dissolution is then limited by the rate at which dissolved dissolution products are transported (diffusion, advection) to the bulk of the solution. Faster dissolution results from increased flow velocities or increased stirring. The supply of a reactant to the surface may also control the dissolution rate, (b) Pure surface controlled dissolution results when detachment from the mineral surface via surface reactions is so slow that concentrations adjacent to the surface build up to values essentially the same as in the surrounding bulk solution. Dissolution is not affected by increased flow velocities or stirring. A situation, intermediate between (a) and (b)—a mixed transport-surface reaction controlled kinetics—may develop.

Fig. 6.1. A schematic representation of a batch reactor for use in a heterogeneously catalyzed reaction. (Reproduced, with permission, from Ref 1.)...

FIGURE 4.3 Schematic representation of process streams during must cooking (upper side). Symbols indicate the steady-state condition (bottom side) L, (kg/batch) is the fresh grape must entering the open pan G2 (kg/batch) is the water vapor leaving the open pan G, and H2 (kg/batch) are the hot-dried air streams w, (kg/kg) is the solid concentration in L, T is temperature (°C). 

FIGURE 4 Schematic representation of the steps taken for data scrutiny. (A) Illustration of the batch sequence showing QC samples analyzed in the beginning and then sporadically through the batch. Test samples should be randomized in sets of 5-10 samples. (B) A peak table from the QC data is examined for peak area variability (filter CV<30%). Variables that show CV > 30% are excluded. (C) Variability of features is examined over the RT and ml axis. Red dots represent features with CV > 30% in the QCs, green dots are features that show CV < 30%. This examination could reveal potential analytical pitfalls, for example, in the case where a load of irreproduc-ible features are concentrated in a specific area. (D) Test samples show much higher variability than the QC samples as shown in the corresponding box plots. (E) When the QC data shows... 

Figure 369. Schematic representation of the layout of a rotary drum coater (Hi-Coater) with a batch size of approximately 200 kg ...

Fig. 4 Schematic representation of the interaction of a representative drug substance with cyclodextrin. A wide range of noncharged and charged (anionic, cationic, and amphoteric) cyclodextrins have been used as chiral selectors, as well as for the optimized separation of nonchiral compounds using capillary electrophoresis. Cationic and amphoteric cyclodextrins are less commonly used in chiral analysis, and only a few are commercially available. The degree of substitution of a cyclodextrin may vary from one manufacturer to another or even from batch to batch, which may have a detrimental effect on the reproducibility and ruggedness of the separation system. (Modified from Ref. 169.)...

Fig. 6.3 Schematic representation of typical equipment for size enlargement by tumble/ growth agglomeration (left) and the post-treatment steps required to obtain a final product (right). Left, from the top Inclined disc (pan), drum, continuous mixer, batch mixer, fluidized bed.

Fig. 7.25 Schematic representation of different batch operating low shear mixers with indication of basic particle movements.

Fig. 8.11 Schematic representation of a batch spheronizing system including mixer, extruder, and spheronizer (courtesy LCI Corp., Charlotte, NC, USA).

Fig. 7. Schematic representation of the preparation and application of catalyst samples for MAS NMR investigations under batch reaction conditions.

The reactor used for starch hydrolysis was a standard two liter Ace Glassware, four-port batch reactor. The central port was used to house the agitator shaft in a jacketed column. The agitator was powered by a variable speed motor operating at lAO rpm. The three side ports were used to house the internal thermistor, a NBS thermometer, and a teflon plug for the sampling port. The reactor was thermostated both internally and externally in a well-mixed oil bath. This thermostated system was found to achieve a desired temperature within three hours and to maintain the temperature within 0.3 C continuously thereafter. A schematic representation of the apparatus is shown in Figure 1. 

Figure 1 shows a schematic representation of the operating principle of a batch reactor likely to be used at very high pressures. 

This in situ ATR-IR investigation of a heterogeneous solid-liquid catalytic reaction gives simultaneous information about dissolved and adsorbed species, which are crucial in elucidating the mechanism of a reaction. Many in situ ATR-IR cells (both batch and continuous flows) are commercially available, and in some cases the cell has been made or modifled in-house to suit specific needs [71]. A schematic representation of a typical in situ ATR-IR setup is shown in Figure 12.8. 

In a closed system, such as a batch reactor, the characteristic property varies with the reaction time. In an open system (such as continuous reactor), it varies with position or space time. In this case, the space time is defined as the ratio between the volume or mass of the reactor system and the inlet mixture flow. The schematic representation of the two systems is displayed in Figure 1.1. 

The polyacrylate used by Sim et al., (2011) is a thermoplastic acrylic copolymer synthesized (Gan, 2005) by free-radical polymerization of six monomer units added in semi batches to the reactor, as described in detail by Zhou et al., (2004). Schematic representation of the chemical stmcture of PAc showing part of the random distribution of the six monomer units viz. styrene, methyl methacrylate (MMA), butyl acrylate (BA), AA, 2-hydroxy ethylacrylate (2HEA), and isobutyl methacrylate (iBMA) in the backbone of the copolymer is shown in Figure 13 (Sim et al., 2009). The alphabets a-f denote mole fraction of 0.16, 0.17,0.39,0.19,0.06, and 0.03, respectively of each monomer unit in the copolymer. Figure 14 displays the difference in the results between a miscible and an immiscible blend systems. 

Hot aggregates, reclaimed asphalt (if used), filler and hot bitumen are mixed for a certain period and the produced asphalt is directly unloaded onto the pending truck or transported by skip to a temporary storage silo. A schematic representation of a batch plant is given in Figure 8.1. 

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